Process of fractionating liquids such as mineral oils and the like



A. R'. EARL ETAL PROCE'SS 0F FRACTIONATING LIQUIDS SUCH AS MINERAL OILS AND THE LIKE April 7, 1931.

4 Sheets-Sheet l Filed Feb. 25. 1927 WITNESS April 7, 1931. A. R. EARL ET Al. 1,799,414

PRocEss 0F FRACTIONATING LIQUIDs sucH As MINERAL oILs AND THE LIKFv Filed Feb. 25. 1927 4 sheetssheer 2 INVENTORS ,-Rarl Z BY .Reeves ATTORNEYS April 7. 1931.l 1,7%,414

y PROCESS OF FRACTIONATING LIQUIDS SUCY.Y AS MINERAL OILS AND THE LIKE A. EARLET AL.

Filed Feb. 25, 1927 4 sheets-Sheet 5 A Earl.

. Reevea,

WITNESS `API 7, 1931. A. R. EARL. ET AL PROCESS OF FRCTIONATING LIQUIDS SUCH AS MINERAL OILS AND THE? LIKE Filed Feb. 25. 1927 4 Sheets-Sheet 4 f EQUALLIZER PPE src/m mLc-r g1 on. INLET smrr. vALvu TEMPonAnY TEMPBRARY aroma: sun/d5 Tue Remwu. 'rmms l TANKS NOZZLE cnuns au v FlLLwc. sy

U TL" GRAvary :xH/w51- rc JET CUNDENSCR 4 l SWIFT INVENTORS .Earl.

ATTORNEY A. MM!" l I l. A 752; www

Patented Apr. 7, 1931 ALFREDy E. EARL .annmrioivms W. nEEvEs, or relleno,l eine Y.

Appiiceaen inea February a5, 19,27. semi No. 170,537.

The inventionrelates toa process of separating a liquid composed of a group of com# ponents having widely separated boiling points, mere specifically dealing with the operation of such components as are found in the various mineral or petroleum oils, and

in regard to gravities ofthe fractions, secondly the utilization of heat which is usually wasted and thirdly a more.,- advantageous method of carrying out the processes of fracv y2 tionatingliquids ofthe class described vand morey expeditiously andr economically i frac` tionating them. l

The process isnotable for its utility, for its v concentration vasto operation, for its tieni-- bility of operation, its adJustability of vary-i ing operating conditions with diminished de-A structiveness ofthe higher grade fractions'. One method, illustrative of the process; is diagrammatically' illustrated in certain fig# A ures ofthe drawings, other figures illustrating the connections, by the various units of the system of distillatiomand of the construction of certain units of the system.

Figure l illustrates diagrammatically ay plan ofthe various still units andthe method 0f connecting these units,

Figure 2 illustrates a diagrammatic flow sheet of one'stage of' the process, showing the products of distillation through various units, 4f Figure 3 illustrates in diagrammatic fashion a flow sheet illustrating` thefpassage of; the vapors through the various still Aunits and through variouscontaining units ofthe system,y

Figure i represents in diagrammatic fashion the crude `oil flow-vapor'ilow and equalizer pipe connections'between the various still units of the system,

- m Figure 5 diagrammatically illustratesuthe u connections between the condensingl yunits andthe temporary storage`tankssliowing diagraniinatically, the` mains introducing` the oils and lsteam to the temporary storage tanks'and the valve connections for. control ling the direction of iow Of eiland steam, and `L I i Figure 6 represents diagrammatically the construction of one of thestillunits, these. still runits being similarly constructed in the several instances. y

Referring first to FigureY 1, there yare shown a series of'heating units for the oil shown diagrammaticallyby members A, B, C, D, E, F, G, and H, these velements constituting the mainheaters ofthe system. 'Mein- 65 berA is a highpressure stillv delivering its vapors throughpipe A-and acond'uit S3 to member E which may be regarded as ay pri'` mary de-superheater still. This still'isy inv fact a preliminary de-superheater and isk connected to pipe Drby thez pipe EU The pipe D is connected between themem'berD and the conduit S5. Asecondary' de-super` heater F is connectedwith the superheater E by a conduit'St. A secondary preliminary heater G vis connected bya conduit S6 and pipe G," G2, and H to a primary heater These various units areconnected in. series as indicated'in l`igs.' 1 and 15, the steam'passage connections betweenv thembeing represented by reference letters S to l S6 inclusive on Fige ure l. Unit D is connected by a pipe D and a conduit S5 to unit G, while units B and C are connected by pipes B, Cand conduit 'S1 to unit F. In' a similar'manner, units D and f8 E are placed in communication withunitG by ineansof pipes D', E", and conduit. S5. Furthermorefunit A is connected .to unit B by a conduit S1; unit B withf unit C by a conduit S',- .andunit C with unit Dby a conduit S3. The connections between members A, B, and C are provided with nozzles tov admit thev iow'of vsteam,these nozzles Vserving for the control offste'am flow .through'the process; which the cross sectional areas S to S6 and proportions thereofsecure to the elements which `they connecti In.practice the flow nozzlesv are threewin number. Thew'first or initial flow nozzleAlOO is connected betweenl the high pressurestill'A and the initial 'supe ion ply of steam at the inlet of the high pressure still. This nozzle controls the volume of steam. The second flow nozzle 101 is what may be termed a ratio flownozzle between the initial flow nozzle and the third and main control nozzle 102. This third nozzle is the main control nozzle, this being where a 55% drop takes place, and controls the Weight in pounds of steam. These nozzles increase in diameter progressively in proportion to the volume of the steam compartments they con-V nect. The succeeding steam connections be.- tween the following stills would likewise increase kin diameter but with fno nozzles inserted in the same. These nozzles form governors which control the rate .of capacity which -has been pre-determined and vas the lad of the process -is constant and does not vary like :the loads of a power plant do, no regulating device is necessary as the flow of steam through these nozzles serves the purpose of a mechanical regulator.` For reference to the subject matter of steam flow nozzles attention is called to Kents Handbook for Mechanical Engineers.

Illustrated in Figure 6 is one of these heating elements the member H having been taken for the purpose or the illustration. It will be understood that the construction of the remaining heating elements are lin each case similar to the particular con-struction, the .ends of the `shell 1 being dished and finalised the convexed side being placed in we ly. A port 2 for the incoming oil is provided :between the lower sheets and the bottom heads. This opening is large enough for a Workman to :enter the still. Similar opening `2 fis provided at the uppermost part of the still.` In the upper part of the still as shown at is an equalizer pipe by meansV of which the oil level in the still and the pnessure therein may be Aequalized with respect to the oil level and pressure in the remaining units. At l is designated a .crude oil outlet. Above the tube sets is provided a space which ris about a v:toot longer than the length of the tubes vand sai-d space is in communication with a conduit G through which fa tube may be removed when withdrawn or replaced. .Connection 5 .delines an exhaust of a jet condenser 135 by means of which a vacuum is `produced in the system.

` The still is supported by members 7 resting upon suitable supports such as concrete `piling 8. The .crude oil inlet to lthe bottom of the .shell 1 is represented by passage' 11. In passage 11 there is inserted a Icheck valve 11'., the obg'ect of this chcckAvalve-is in case a vacuum in the `system should be broken the variant .oillevels of the severalstills would Seek. a natural level overflowing through the constant level tank also at the outlet of the high pressure still. The tubes 9 of the still are heldin place by tube-.sheet `stays 10.' The primary connection is piped tothe initial that leads downwardly to the bottom-most compartment of the preceding element, and so on consecutively, the several elements being connected by pipes 4, la, 41", L1B, 4d, le and 4f. .The pipes .thatconnect .the high pressure still element with the lirst intermediate still element, :the second intermediate still element with the low pressure still element, also the secondary de-superhea-ter element -with the secondary preheater element h-as incorp0rated therein a ,quick opening gate valve.

An oiloutlet slightly above the vtop set ol' the primary element which is the high pressure still element, is piped at 103 to an oil trap 104 .that discharges into va regenerative still element 1.

The Jour still'elements have steam traps 105, 106, 107, 108, respectively connected to the steam compartment externally of the tube elements; also the four de-superheater and pre-heater elements have oil traps 109, 110, 111 and 112 likewise connected.

As illustrated diagrammatically at Figure 3 the last element of the series is AConnected to a constant level-feed tank T, the construction of which does not form a part of the present invention.

' vThere are also provided regenerative and refrun still elements 1, J and "K, which are cylindrical tanks with vertical towers upon the same and these tanks lie horizontally iinclined as shown in Figure 2. These elements are to be in duplicate and to alternatel in operation. There are of course the necessary fractional oil inlets 103, 120, 121, 122, and 123., steam inlets 125, 126, and 127 and at the upper-most part of the towers or domes vapor outlets 128, 129, and 1.30 provided with the necessary valves and connected to the succeeding order of the system. This con struction will be obvious to anyengineer who is familiar with the installation oli' such .sys-

tems to whichthe present system relates.

This construction of the regenerative steam stillelements is identical in the rectify'ing Vsteam still element; residual cil pipe lines, with necessaryfvalves that are required, lead lto containers 131, 132, and 133 of ample capacity and strength, lfor temporary storage, before the liquids'are placed in permanent storage.

The containers are in duplicate for like .rract1ons,- and 1n dual connection-s by piping and necessary valves, for oil and steam inlet, likewise oil outlets, in order to provide for flexibility for alternate and periodic 'operations of the oil disposal.

Vapo-r pipe lines leading from the regenthe like andthe oil overflow is piped to 'theY ,densed.

' ation condensers 143which comprise drum orerative, secondary re-run, still elements, vwith necessary valves for shunting the vapors at the will of the operator, discharge their content back to a predetermined stage in the pri'- V mary separating element, or, either indirectly into the steam condenser through-tlie-nievdium of integral, consecutive., coiled pipe condensing elements 136 or 137, submerged in watery in the-tank,- with a water inlet and outlet; the A condensed vapors collect inl containersll to 133 inclusive and f the funcondensed vapors 'pass through pipe equalizer elements into the y steam condenser 135. VrEhe connections are shown diagrammatically in the accompanying drawings and will be obvious to tlie-individual skilled in this art.

' The steam condenser 135 mentioned herein and shown diagrammatically in the drawings is'preferably of the'low level jet type, the same forming no part of the present invention. It is however, of the type which lifts its ownk injectionv water, and whichfis provided with al submerged removal pump discharging its condensate into aseparating tank 140. `The air'pump 141 is of the compression e type and may be either rotated or recipro-x cated,y Said pump discharges its'content to submerge it in the same separating tank. Thewater overflow of this tank isto be used in connection; with a pipe coil condenser or receiver lof a receiving pump 142 that discharges the content to storage or other disposal. 1 y

There` are also provided atmospheric radicyl'indrical tank elements, with concave heads and manholes; the condensers being connected togetheriwith an intermediate ltube element andset horizontally inclined for drainage.` f

pounds absolute', 145 pounds gauge, and with i a practical super-heat et 300O F. iiows Jfrom a 45 pressure still element into the irsty interme-f diate still elementi` The steam so iowing,'undera predetermined reduced pressure, by v means ofy the :flow nozzles, would rexpand toy any increasedvolume', proportioned to the reduced pressure and a partial' liberation ofthe steams total heat content, relative to the pressureand tempera-ture so reduced, would result. The steam so expanded, internally ot the steams compartment, and externally oit the tubular element, within 'the steam'com- Steam, at areasonable pressure oit 16()l partmentoi:I therstill element having its heat content partially liberated, represents the secondary initial pressurel in the irs't'intermediate still element. f f The heat content so liberated, travels "by conduction and convection, throughlthe steam vapor, the metal of the tubular lelement and l the oil, internallyof the tubular element,y aui `tomatically seeking the thermal equilibrium of a natural temperature balance.

Steam having flowed through the initial How nozzleand down through the steam compartment of a highpressure still, discharges through the iow nozzle7` connectingy the lhigher pressure still with the lirst intermediate, then up through its steam compartment and discharges through the mainfcontrol nozzle into-the second intermediate still,l down through its steam ycoimoartment and discharging-through a connection into the low'pressure'rstill, thenV up through its steamcompartment dischargingV through a connection into the primary cle-superheater then-` down its compartment andthrough a connection into a secondary de-superheater up its compartment and through a vconnection tov the `rsecondary pre-heater downits compartnient and discharging through a-fconnection to a primary pre-heater, upV its compartment and discharging throughl a vconnection tothe standard type` of jet condenser 135 to be con-V vThe steam so flowing will have increasedy its volume from 4.15 cu. ftper pound tol 272 cu. ft. ,the pressure will'drop from 160 pounds absolute to 1 pound absolute and the temperature will drop from 6630 F. to 109o l".

The totalf'heat of steam will drop 'from 1350 i B. t. u. perpo'und'to 1108 B. t. u., 242 B. tl. u. Q

liberated per pound ofy steaniflowingand absorbed by the oil ;`the`latent heat ofthe steam i to be condensed willbezlOBQ'B. t. u. per lb., the condensing water will absorb 3() B. t. u.v per lb., and 34 lbs. of condensingl water will"v be required per pound of steam. f

It the initial flow nozzle is assumedv tentavtively to be eight inchesin diameter, with 50 square inches of area, then the steam-pressure and temperature mentioned will have ave-` locity ot approximately" 8600 feet per minute,y

and the weight ci steamwill be a oroxin Y y mately 40,000y pounds per hour.- y

The volume ratio iiozzle,1nain controlA nozn zle, their connections, and the consecutive succeeding connections', yalso the volumetric content ot the steam compartments would be relatively vproportionall fory a unit, through which lthe steam would iowl approximately alongthe theoretical Aadiabatic 'expansions-V- curve line ofno heat transmission.'

The heat required to raise the boiling-'point 'of Ithe oil `from the iirst intermediate stilll element tothe boiling point in the high pres-fv sure. stillelement plus the latent'heat'of va-` porization of the fraction so Vaporized, would for the unit.

be Supplied by the heat liberated by the steam, expanding through the highv pressure still element, and a natural heat exchange takes place by Way of a temperature balance.

The heat required by the. fraction to be vaporized and the heat liberated by the expanding steam inthe high pressure still element would be in a ratio of 1 to 1.71, or approximatelyy 600 pounds steam per initial barrel of 350 )ounds crude ietroleum and the governed by the flow-nozzles, and in principle is'approximately the same as in a steam turbine. Y

Crude petroleum, to be distilled, flows by .gravity to the constant level feed tank, from Where it is drawn inductively by the vacuum maintained by the steam condenser; and the altitude ofthe column of oil in the several elementsl Will be proportional to the vacuum, into which the vapor lines of the elements discharge. .p v p f The vacuum in the oil compartments of H. and G. Will be 27 .5 inches mercury; the same as it is in the steam compartment of H. into which the equalizer vapor lines lead, and the Apotential hydrostatic head of the column of tank.

oil so supported Will be 39 feet and six inches above the oil level in the constant level feed The vacuum in the oil compartments of F. E. and D., will be 25 inches mercury, the same as the steam compartment of G., in which the equalizer vapor` pipes of F. and D. lead, and the altitude of the column of oil so supported Will be 34 feet and 9 inches, and the difference of altitude, or flow head between G. and F. Will be 4 feet and 9 inches, as a kinetic head. The pressure in this case is absolute..

The vacuum inthe oil compartments of C.- and'B., Whose vapor lines lead to the steam compartment of F., Will be 19 inches, and the column, offoil sosupported will be 26 feet and 9jinches, and thedifference of altitude of the oil columns between D. and G. Will be 8 feet, as a kinetic head.

7 The roil compartment of the element A whose vapor line discharges into the element E. will be at a pressure of one atmosphere and its oil level will be at 1 foot above its upper tube sheet, and maintained there by the over-How outlet, that discharges throughl a tloat valve into the regenerator, and steam ,still element I..

still elements A. B. C. and D., due tothe heat liberated in the steam compartments of same, there Would be a tendencyl to unbalance the potential heads, which Would immedi-y ately be replaced inbalance consecutively by the higher potential heads of the succeeding elements; and ultimately more oil, propor.

tioned to the amount vaporized, Would be' drawn into element H. from the constant level feed tank in a natural hydrostatic balance.

As vaporization of the fractions of the initial crude petroleum would be the factor element, from which the fractions Were va-A porized.

As the oil feed is induced, andthe unvaporized fraction. flows away by gravity, no pumping is required by the primary separating element.

In the first four elements, A. B. C. and D. the oil flow Would be turbulent, due to the ebullition, While in the four remaining elements-E. F. G. and H. a quiescent flow would obtain. f 1

Mid-continent crude petroleum of .8000 specific gravity, .5000 specific heat, Weighing SSOpounds per barrel, at a temperature of 32 degrees Fahrenheit, is assumed to be progressing through the process. Y

The oil will be raised in temperature 77 F.,`from 32 F. to 109 F. by absorbing 35 British thermal units per pound, as it passes through the primary pre-heater H. to the secondary pre-heater G. Where it will be raised 24 F. from 109 to 133 F. by absorbing 15 B. t. u. per lb.; then through the secondary de-super-heater, Where it Will be raised 32 F., from 133 F. to 165 F. by absorbing 17 B. t. u. per lb.; then through the primary de-super-heater E. Where it Will be raised 47 F; from 165 F. to 212 F. by absorbing 28 B. t. u. per lb., and Where some gases-butane, pentane, and the lightest naptha, will distil through the vapor line of the primary dessuper-heater E.

The oil, then passing through the low pressure still D. Will be raised 1 F. from 212 F. to 213 F. Which is the theoretical for saturated steam, When highly super-heated steam expands through a turbine, pressure reducing-valve, or an apparatus of the nature herein described, the heat content of the vapor is not relative to the temperature, and this condition is called super-saturation or an unnatural super-heat, and the steam is said to be cooled-as the heat content of the vapor is greater than its temperature.

This condition would exist, beginning inV the lovv pressure still, Where the initial steamV pressure will have been reduced to atmosioo i '.pheric and continue through the two desuper-heaters, as a natural condition of the steam, which will be further intensified by the hot oil vapors flowing from the high'pres.- sure still A and confluently withthesteam through the primary de-super heater E'.

. Also, the vapors from stills B and G flowing jointly and confluently with the .steam through F; the actual amount'oi" his condif tion is unknown.

It is assumed, for simplification, that the specific gravity and heat remains constant at .8000 and .5000 respectively, throughout the process, and no unavoidable radiation heat losses are considered; thev sensible heat 01: liquid content of the oil is deducted by the analogy of water' at like temperatures, and the llatent heat of vaporization is empirically deducted from the 'meager information on the subject, by Mabery and Goldstein, and published by Bacon and HamonjAmerican Petroleum Industry, vol. 1, page 108,5th impression. f

The vapors counted for, as the `oil progresses 'from the element E to the element Dor a temperature of 213 F. due to the subfatmospheric pressure Within the oil'compartment oi' D. f

As the average boiling point-200 Fffat atmosphere, of the light naptha fraction has been reached and passed, ebullition will take place, and seven perl cent,`or by weight, 24.5 lbs. of the initial 350.lbs., per barrel, .will vaporize; the-latent'heat, assumed at 160 B. t. u. per lb. will total 3920 B. t. u. for the fraction of 24.5 lbs. and the heat of liquid will be 90 B. t. u. per lb., and total 31500 B. t. u. for the initial 350 lbs. oi'oil per bbl., the 160 B. t'. u. latent heat, plus the 90 B. t. u. heat of liquid, equals 250 B. t. u. as the toal heat of the vapor per lb., multiplied by the 24.5 lbs.

vaporized, equals 6125 B. t. u. as total heat of the fraction, of which 3920 B. t. u. oflatent heat must be removed for thephysical .change of state of condensation. 1

The remaining ninety-three (93%) per cent, or 325 lbs. of oil, with a boiling point above the temperature 213 F. within the low pressure still D, advances to and through the second intermediate still C. l

AWhere its temperature is raised 165 F. `Vfrom 213 F. to 37 8 F., by absorbing 85 B.

t. u. perlb., for the total 93%,*013255 lbs.

of initial crude residue from the low pressure still D., the equivalent boiling point due-to the sub-atmospheric pressure, specific to the secorfd-intermediate still Cpwillbe 425 F. and the crude heavy'naptha fraction, Withan average boiling point vof 300 F. atmosphere,

' will vaporize 14%or 49lbs., withlatent heat assumed at v155 B. t. u. per lb., that will total 7595 B. t. u. for the fraction, plus 857 5 B. t. u., as heat of liquid equals 16170 B. t. u. heat content of the vapor leavingthe still 7.9%

leaving the primary de-superheater Ev are trivial 1n volume and not ac' or 276.5 lbs. unvaporized asresidue or still G. will advance to and through the first intermediate still B. f

boiling pointot450 F. will vaporize 17% 'K or,59.5 lbs. will be the amount of the fraction,

and its `latent heat assumed'at 140B. t. vu.

perlb. will total 8330 B. t. u. the total heat content 'of the vapor'will be 25109 B. t. u.

for the fraction; the remaining 62% or 217, lbs., as residue of still B. will advance to and through the high pressure still A.y

Y -lVhere its temperature will be raised 93 F. from 570 F. to 663 F. by vabsorbing 68 B. t..u.perlb. for the total of 217 lbs., the

total heat of liquid will be 350 B. t. u. perk l lb., and the gas fuel oil stock, with an avere age boiling point of 550 F. will vaporize 20% or 70 lbs. will be'the fraction, and with the latent heat assumed at `130 B. t; u. yper lb., the total latent heat of the fraction'will `be 9100 B. t. u. and 33600 B. t. u. the total heat content of the vapor.

- The vaporization now totals 58% Lor 2,03.

lbs. and the residuumof 42% or 147 lbs. at a temperatureof 663 F. and lwith 350B.:t. u.-

per lb. as its heat of liquid content, which lowsby gravity through an oil trapto the Y lamp distillate, regenerator, re-run, tar still; the primary separation, or iirst stage of the process is now complete. Y l

' It yis observed that the temperatureof the oil, and steam`,fis the same for the-same element alsothe temperature drop in the steam,

and the rise in the oil, by degrees, likewise the B. t. u. (British thermal units), as per the speciiicheat mentioned.

' The heat of liquid content, of the steam compartments, are for saturated steam at that temperature,'and'correspond to pressures oi' 2361, 1200, 192 and 15 lbs., absolute,

in the super-atmosphericv elements A, B, C and D, and 14.7, 10, 5, and 2.5 lbs., barometric in the sub-atmosphere elements, E, F, G, and y H; it is understood that these high pressuresr are fsubstitutedby the superheating of the steam 300 F. at 160'lbs.. absolute.

'lhe hot vapor flowing at a temperature of 663 F. from still element A enters the steam compartment of the cle-super-heater element E and iiows jointly with the 4steam atv its temperature of 212 F. .the diierence `of temperature between'thetwo vapors is 450 F.and a temperature balance will take place, whereby the oil vapor Will be condensed, and

the steam slightly super-heated'byA the 9100 l B. t. u'. latent heat of the fraction-absorber by the 596 lbs. of steam (required to vaporize it inthe still element A) as its equivalent v passes through the element E.

. The vaporsowingfrom still elementslA respectively, and then jointly and confluent with the 596 lbs. of steam at its temperature of 165O F. as they pass through the de-,superheater element F; a temperature balance will take placewhereby both oil vapors will con.- dense; the condensate of the oil vapors mingle, and a re-evaporation of a part of the lower boiling point fractions, of the chain, of vaporfrom still element C Vwill take place, due. to the excess. heat of liquid content, of the liquid condensed from the oil vapor from still elementA B this vapor of re-evaporation will flow along with the steam, to the preheater element G.

The vapor-s flowing from the still element D and de-superheaters E and F at temperatures of. 213O F. 212D F. and 165o F. respectively, and jointly, confluent with thesteam vapor at itstemperatnre of 133.0 F. a temperature balance will take place whereby the high boiling point fractions of the. vapor from element 'D will condense; vapors of low boiling pointV fractions. and water vaporized in the oil, will pass through the vacuum equalizer pipes' confluent with the steam in pre- Y heater element H. andthen to an atmospheric radiation condenser, at a temperature of 109 F. andlif the atmosphere temperature be `assumed. at o F. the difference of temperature is 19O F; and the radiationassumed at 1.75 B. t. u. per square foot, per hour, for each degrec of difference, then the heatv lossby radiation will, approximately be 33 B. t. u. per s uare foot, per hour; if the injectionY water o the steam condenser be assumed at 70o F., and the condensate at o F. the tempera,- turehead ofthe condenser will be 9CJ F. and the condensing waterwill absorb 30 B. t. u.

per lb. Evidently each square foot per hour of atmospheric radiation will be Vequivalent to one pound of water less-to be supplied by the condenser: (refer to 1922 trans. A. S. M. E.-page 299; for heat losses from bare pipe) the latentheat of the steam will be 1108- B. t. u. per lb. for 596 lbs. of steam perfinitial barrel of oil.

It is understood that the boiling point of liquid, and the condensing point of. its vapor, always agree for any given pressure and temperature, as the radiation heat loss is un` known, definitely, it is not'considered, and alli of the fractions are assumed to be at their boiling point.

The 42%, or 147 lbs., residue from still element, A. and the 17% or 59.5 lbs. of lamp distillate from de-super-heater F. flow inductively and confluently into the regenerative lamp distillate still element I by virtue of the lesser subatmospheric pressure within same; as the intermediate gas fuel oil fraction has been isolated. from same, the difference of'liquid heat'content willbe 68 B; t. u. per lb. between the two liquids, above the lamp distillate boiling point, and totals 999GB. t. u.

. rectifier J. and then discharged from same to for vthe 'residue fraction as heat ofconversion, into latent heat of vaporization, for the lamp distillate, that requires only 8330 B. t. u. per fraction. 1

The lamp'distillate vapors, rising in the stills tower element, flow inductively vby Virtue of lesser pressure and confluently with the steam, in the pre-heater element G wherein a temperature balance will take place'and the distillate condense. The condensation flowing by gravity to thelamp distillate rectifying steam still element J., until the predetermined oil level in same is reached; the condensation sov fiowing is then shunted to the duplicate element. Steam at a temperature of 663 F. is injected into the filled still, until its temperature has reached the boiling pointof the gas-fuel oil. fraction; this will be 447o F. as the equivalent boiling point of the 550o F. average boiling point at atmosphere.

The lamp distillate vapors, rising in the stills tower, eXits through a vapor line, connected consecutively to a submerged pipe coil or the like; condensation takes place and flowsby gravity intoa container element until the pre-determined liquid level is reached.; the stream flowing into saine is then shunted to a duplicate element; saturated steam is now injected into the filled container until its temperature reaches: 847 F. the'equivs alent boiling point of the 450o F.V average, atmospheric boiling point of the lamp distillate fraction; the volatile, low boiling point fractions of the kerosene chain, will be vaporized andV flow jointly with the steam, to the condenser; the lire` test of the kerosene residuum will be raised, and when cooled'below the ash point, discharged from the container' to storage or treatment. v

Thegas fuel oil fraction, of 20%, or 70 lbs. and the heavy naptha fractions, of 17% or 49 lbs., flows by gravity,.from the primary de-superiheater E. and primary pre-heater H. respectively, and confluently within the regenerator naptha still element K.; their temperatures will be 663O F. and 3780 F. respectively,A and their relative heat of liquid content, 350 B. t. u. and 175 B. t. u. per lb.- a difference of 175 B. t. u.-du.e to the isolation of their intermediate, lamp distillate fraction. This difference is in excess of the latent heat or vaporization, of the heavy naptha fraction, at a boiling' point of 378 F. and re-evaporation of the naptha will take place; the vapors flowing directly to the steam condenser.

l/Vhen a predetermined liquid level has been reached inthe regenerator element K saturated `low pressure steam is blown through the gas-fuel oil residue therein and same is cooled, below the flash point, after which it is drained, into a container element, jointly with the kerosene bottoms from the storage, or treatment.

The coil pipe condensers, or like, are submarged in tanks of comparatively diminished 'water space, :which is. maintained at a con- 1 stant level by a float valve means, that replenf ypoint of water at atmosphere-its latent heat ish the tank as fastas the water in same evaporates; the water coming from the separating -regenerator distillate ystill the vapors are 'tank,.of the steam condenser, is assumed to .be 1000 F.; to raise it to 2120'F. at atmosphere would'require112 Bqt. u. per lb. or p n the sensible heat of liquid of the oil at'6'30 from 68 to 180 B. t. u.; the vlatent heat of `vaporization is970 B t. u., approximately Aninetimes the4 sensible heat ofthe liquid; as

the temperature ofthe vapors in these coils `is considerable in excess of 2120F., vaporisation of the water in the tanks would take place, the lowest condensing pointv of the `vapor would befrelative to the vacuum. of 27.5 inches, the equivalent condensing point would be raised 1030 F. to 3150 F. and any fractions with a boiling point lunder 3150 F. wouldwnot condense in the coil, but pass through and flow to the steam condenser.

When the 42% -.or 1117 lbs. of tar residue flowing from the high pressurestill A has reached, a pre-determined liquid level in the shunted by valvesvM from ythe pre-heater element G to the coilcondense'r L,which is connected directlyto the steam condenser and a container element, f

. `Steam, at a temperature of 0630 F. is in-A jected'int-o theV residue fractions, within the regenerative still element l its equivalent boiling point Will be 7500 F. due to the vacuum maintained by the steam condenser, through the coil condenser medium, vaporization will take place ;-the oil vapors flowing with the steam to the coil condenser, the 1% or 111 lbs. 'of coke per fraction remaining in the still element l, and willaniount to approximately 11 tons per 2er hours, for a rate .of 06 bbls. per hour, throughout the process. Y

. The heat of liquidthat has been us'edvto regeneratethe lamp distillate, will have to be replaced; it amounts to the latent heat of vaporization of the distillate,--which` is 8330 B.t.uf.; the latent jheat of the 13.3 lbs. of liq.- uid residue is assumed at B.,t. u. per lb. and for the fraction, totals 997 5, B. t. u., plus the heat replaced, totals 183,05 B. t. u. required by the steam,'per fraction.

The high boiling point of the fraction is assumed at 7000 F., 'and thev equivalent tem-k perature ofthe steamr 7660 F. Therefore, 33 B.,t. u. will be available, above v'7000 F. perlb. ofl steam, and 555-lbs. (weight) of steam will bey requiredfor vaporization of .the fraction.

. The steam 4and oil Yvapors flow jointly,

through the paraffine vapor line, tothe coil condenser, and the total heat ofsame will 'be the total" heat of steam at 6030 F.-which is 1350 B. t. u. per lb., the heat exchange beingsimply a latent heat transfer 'fromthey steamtothefoil, byV virtue of the condition absorbing v,equivalent being 2120 points of their chain condensing in the atmosof vaporization is 970 B. t. u. per lb. whilep rthe total heat ofthe steam and oil vapor -flowingthrough the coil'will be 13.50B. t.u.k

er 1b.#a dinlerenceof 380 B. t. u. per lb.;

F. is 350 B. t. u. and at 2120 F.90 B. t. u.j-

a difference 0101260 B. t. u. per lb.-

In a natural temperature balance,` with the water at 2120'F. 380 Bft. u.-plus 260 B. t. u.-a total' of 640 B. t."u. per lb., will have to be disposed of bythe water, with an capacity of 68 B.` t. u. sensible, from. 1000 F. to 2120 F.' plus 970B. t.v u. latent, or 1038 B. t. u'. per lb., above 2120 F. the oil vapors 'with a'condensing point above 2120 F., or the equivalent ofv 3150 F.,v

would condense, and the liquid lof oondensa- .-tion, 38%,

or 133 lbs. would liow tolthe container as 22% paraiifine distillate;f15%

cracked distillate; and 1%1waX tailings, at

aftemperature of 2120 F .;the 'cracked fractions, witli a boiling point below 3150 would flow through the coil condenser, along with the steamv uncondensed,"to the steam condenser, through theniedium of the n atmospheric radiation condenser. y

of the steam will The 1 total heat content have been reduced`199 B. t.'u. from 1350,'at

y6030 F. to 1151,r at 2120 F. by the'coil condenser, then flowing to the steam condenser, with 1151 B. t. u., at 2120 F., carrying with it such fractions as may occur, with boiling points below 3150 F. to be condensed. The container isthen discharged" to storage, the cracked fractions separatedy from the paraffine'fractions by settling, and return with the initial` crude petroleum.

The'napthas of the primary separation and :fe-run, cracking fractionation, are condensed with the steam at 1090 F.,-the F.; the higher boiling the pressure in thechamber before the ori lice of samereduced to 55% ofthe nozzles initial pressure, will deliver a constantvolume of steam, regardlessof any variance,

below the critical pressure. and is the govY ernor ofthe rate 0f capacity ofthe process.

y u andb'ased on l a definite size of pipe, steam,`pressur'e and temperature, for a steady flow, 'and wfith ,125v

2.'. Crude petroleum drawn` into the process by virtue of the sub-atmospheric pressure within same, to varient altitud'es relatively proportional to same, in hydrostatic balance; a quiescent flow through the process, inductively, until changed toa turbulent How, by virtue of the ebul'lition, with a consequent, vaporization, reduced and unbalancedv altitudes, with potential Vhydrostatic heads, changedv to kinetichead's land adjustment of same, automatically continuous.

3. The lirst stage of the process is dry or cracking distillation, for a large yield ofl burning 011, for combustion purposes, which take place as the primary separation.; the-second stage is with steam in direct Contact, for the minimization of decomposition of the high gradelubricating fractions, and takes place'as the secondary fractionation, through the process of vaporization and subsequent condensation in steam; regenerative re-evaporation in oil', and ref-condensationv by dissipation of its latent heat of vaporization, through the medium of air of the atmospherey and water.

4. As the oil vapors of the primary separation are condensed in contact with steam, mixed with same, at a lower temperature, also a lower condensing point, the higher boilingl point oil' vapors will condense, relatively with lthe temperature of the steam which does not condense, butiiows on in its course, carrying with it the lower boiling point` oil vapors, to af succeeding' stage of they process, of less temperature, untilV the fractional condensation is complete.

5. The liquids of two condensed. vapor fractions, of widely differing boiling points, due to the isolation of their intermediate boiling point fraction, are mingled together, each at or near their respective boiling point and with a lower surface pressure; the excess heat/of liquid. content of the higher bo-iling point fraction converts into latent heat of vaporization, for the lower boiling'. point fraction and vaporization of samev results, withl the lowered heat of liquid content, of the higher boiling point fraction, proportional to the temperature balance; and the heat exchange is at a much higher temperature than would be possible-in a natural ebullition, and the cracking or disassociation of the fraction so vaporized intensified.

6. Vapor fractions, with a chain of boil'- ing points at high temperatures, pass through coils, or the like, submerged in water, which iskept at its boiling point by the heat of the higher temperature of the vapor, exchanging with and vaporizing the l'ower boiling point water, at itsatmospheric vaporizingtemperature.

The heat absorbing capacity ofthe water is increased; and its minimum and'max-imum temperature equal and constant. The vapors being in vacua will havean equivalen-t. convdensing point, relative to the' temperature of the water, proportionate toy the-vacua; and

the. lower boiling points of the. chain in the the fraction, with condensing points above the maximum temperature of the water, boiling at atmosphere, will condense, and. en'- train by gravity to a container, for disposal'.

7. When one of the containers, that are duplicated for each fraction,.is ii'lled,the entrainment of the fraction is shunted to the other; steam at areduced pressure and temperature turned into the container', on top of the oilf forms a steam piston, which forces the oil to egress at the bottom of same, throughy pipes leading to storage or treatment.

The contrast of volumes, for equall weight of steam and oil, is evidence of the practicability; and the continuity of dispatch'vl without pulsation desirable. All. fractions'arere'- run continuously, except the lowest boiling point fractions which are. carried 'along jointly with .the exhausting steam tothe jet condenser. The residuum that goes. to the cokingstill periodicallyl is also an exception to the continuous re-run of the fractions- 8. The constant-.level feed tank'maintain's a constant altitude relative to the several variable altitudes within the several elements of the process, pro ratav to the sub-atmospheric pressure within'the same element,and is changeable'only'by the vaporization, which dominates the How through the process of constant altitudes.

9. The heat content of unavoidable heat loss, due to temperatures below the utility of the process, but above the atmosphere, is partly dissipated to the atmosphere, when fractionations of its vapors are not required in the processand the amount ofwater for condensation, in the final disposal, is mini- Inized.

Brieiiy stated, the process is as follows:

vThe oil entering the bottom zone of still H is assumed to be at 32 F. and therefore contains 16 B. t. u.s of heat per pound. 350 pounds of oil is the unit of weight used as a basis for the following calculations. As the oil flows up throughy the steam zone, which is the upper. part of the still, it will be observed that the various properties of the steam so passing through the still are indicated' diagrammatically on Fig. l. The little vaporization that takes place in the first four stills,.due to the vacuum and consequently reduced boiling points,is not considered as of consequence, but isfconsidered1V as a product from still D and is known as light crude naphtha'. As the; temperature. of the oil progressing through stills l-I, G, F, and E, has been raised in temperature to a point corresponding with the boiling point of the first fraction, the second fraction of still C represents heavy naptha, due to the higher temperature of that still.. The natural lamp distillate uil be vaporized in still B, and in still A, the fraction of fuel or gas oil Will distill over.

lt is to be understood that the oil passing through pipe il, shown in t3, will rise up through the tube and above the top sheet of the tube 9 to a predetermined height as represented on the flow sheet by the indicia Top oil zone. The steam flow through the still A and through the remaining stills has its temperature successively lowered to the final. still l-l. The oil which is drawn into still H has its temperature graduallv increased until it reaches the maximum in still A from Which the residue or the last fraction is Withdrawn. llt will be noted that the oil flows in an opposite direction to that of the steam and the vapors from the oil; that the pressures in the various stills are so varied that the oil from the preceding still Will be draWnvinto the succeeding still at a progressively increasing temperature, While the steam moving in the opposite direction has a progressively decreasing temperature. rlhe steam expands giving up its heat until it is discharged from the initial still H.

We claim:

l. A process Vfor separating hydrocarbon oils into its component fractions which coinprises maintaining in a series of interconnected units progressivly varying pressures, a portion of the series of units having pressures above atmospheric, an intermediate unit of the seriesbeing at atmospheric pressure While the remaining portions of the units being belovv atmospheric pressure, introducing the oils into the units of the system by-means of the sub-atmospheric pressures in oneY portion of the` series of units, causing superheated steam under pressure toiiovv rthrough the first-mentioned portion of the series of units While permittingY the steam to expand in `those portions of the series of units which have a pressure below atmospheric and utilizing the pressures of the steam in the different units for maintaining levels of the oil at variant altitudes in the unit system, said levels being relatively proportional to the pressures in the respective units While maintaining a quiescent flow of oil through a portionv of the system, removing` certain of the component fractions of theunits from the unit in which is contained the greatest vacuum, then separating and recovering the fractions obtained from the last-mentioned unit. v y p 2. A process for separating hydrocarbon oils into its component fractions which comprises maintaining in a seriesof interconnected units progressively varying pressures, a

yport-ion of the series of units having pressures i at variant altitudes in the unit system, said levels being relatively proportional to `the pressures in the respective units While maintaining a quiescent iiovv of oil through a portion of the system, removing certain of the component fractions of the units from thej unit in which is contained the greatest vacuum, then separating and recovering the fractions obtained from the last-mentioned unit. Y

3, A process for separatinghydrocarbon,vv oils into its component fractions which comprises maintaining in a series of interconnected units progressively varying pressures, a portion of the series of. units having pressures above atmospheric, an intermediate unit ofv the series being at atmospheric pressure While A the remaining portionsrof the units being belovv atmospheric pressure, introducing the oilsinto the units of the system by means of the sub-atmospheric pressures in one portion: of the series of units, causing superheated steam vunder.pressure. to iiow throughthe first-mentionedv portion of the series of units While permitting the steam to expand in those portions of the series of units which have a pressure below atmospheric and utilizing thepressures of the steam in the different units for maintaininglevels ofthe oil at variant altitudes in the unit system, said levels being relatively proportional to the pressures in the respective units, removing certain of the component fractions of the units from the unit in Which is contained the greatestvacuum, then separating and recovering the fractions obtained from the last-mentioned unit. c Y Y el.' Aproeess for separating hydrocarbon oils into its component fractions which comprises maintaining in a series of interconnected units progressively varying pressures, a portionof the series of units having pressures." above atmospheric, an 'intermediate unit ofk the series being at atmospheric pressure While ico iio

the remaining portions of the units being belovv atmospheric pressure, introducing the oils into the units of the system by means of the sub-atmospheric pressures vin one portion of the series of unitseausing super-heated steam under pressure-to fiovv through the series of units While permitting the steam to @Krane in those portions et the Series of units which have a pressure below atmospheric and utilizing thepressures of the Steam in the clifferent units for maintaining levels of the oil at variant altitudes in the unit system, said levels being relatively proportional to the pressures in the respective units, removing` certain of the Component fractions of the units from the unit in which is Contained the greatest vacuum, then separating and recov- 1Gering the fractions obtained from the lastmentioned unit.

ALFRED R. EARL. THOMAS W. REEVES. 

